JP2010162510A - Desulfurization apparatus by sea water - Google Patents

Desulfurization apparatus by sea water Download PDF

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JP2010162510A
JP2010162510A JP2009008391A JP2009008391A JP2010162510A JP 2010162510 A JP2010162510 A JP 2010162510A JP 2009008391 A JP2009008391 A JP 2009008391A JP 2009008391 A JP2009008391 A JP 2009008391A JP 2010162510 A JP2010162510 A JP 2010162510A
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seawater
air
liquid
aeration
exhaust gas
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JP5186396B2 (en
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Kiyohito Otsubo
清仁 大坪
Naruyo Nagase
成世 永瀬
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IHI Corp
IHI Inspection and Instrumentation Co Ltd
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IHI Inspection and Instrumentation Co Ltd
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Abstract

<P>PROBLEM TO BE SOLVED: To accelerate the oxidation of SO<SB>3</SB>in a waste liquid containing sulfur with a simple apparatus structure and to reduce COD to a predetermined value or less and increase DO to a predetermined value or more. <P>SOLUTION: In a desulfurization apparatus by sea water including a mixing vessel 15 generating a mixed liquid 25 of which pH is adjusted to 5.7-6.5 by mixing the sea water 6 with the waste liquid 10 containing sulfur, and an aeration tank 18 carrying out aeration by introducing the mixed liquid 25 in the mixing vessel 15 and jetting the air from a plurality of jetting openings of an air pipe 19 provided at the bottom part for aeration, the diameter of an air jetting opening installed to the air pipe 19 is 2 mm or more. <P>COPYRIGHT: (C)2010,JPO&INPIT

Description

本発明は、簡略な装置構成にて硫黄を含有する排液のＳＯ3の酸化を促進させ、ＣＯＤを所定値以下に低減すると共にＤＯを所定値以上に高めることができるようにした海水脱硫装置に関する。 The present invention promotes the oxidation of sulfur-containing waste liquid SO 3 with a simple apparatus configuration, reduces COD to a predetermined value or lower, and increases DO to a predetermined value or higher. About.

近年、環境保全の問題からクリーンエネルギーの開発が進められている。しかし、他方では技術的あるいは経済的な理由により、従来より行われている化石燃料を用いた発電等が現在でも多数稼働している。   In recent years, the development of clean energy has been promoted due to environmental conservation problems. However, on the other hand, a number of conventional power generation using fossil fuels is still in operation for technical or economic reasons.

石炭等の化石燃料を燃焼した場合には環境保全の面から、排気ガス等に含まれる硫黄を除去するための脱硫装置を設置する必要がある。脱硫装置には様々な形式のものが存在しているが、化石燃料を原料とした大型の発電所等では大量の冷却水を必要とするために海に面した場所に建設される場合が多いことや、脱硫処理のランニングコストを低く抑えられることなどの観点から、海水を利用して脱硫を行う海水脱硫が近年注目されている。   When fossil fuels such as coal are burned, it is necessary to install a desulfurization device for removing sulfur contained in exhaust gas and the like from the viewpoint of environmental conservation. There are various types of desulfurization equipment, but large-scale power plants that use fossil fuel as raw materials often require a large amount of cooling water and are often built in locations facing the sea. In recent years, seawater desulfurization, in which desulfurization is performed using seawater, has attracted attention from the viewpoints of reducing running costs of desulfurization treatment.

化石燃料を燃焼させて生じる排気ガスを海水脱硫する場合について説明すると、化石燃料を燃焼させて生じる排気ガスには、ＳＯ2などの形態で硫黄が含まれている。排気ガス脱硫装置は、排気ガスと海水とを気液接触させて、排気ガス中のＳＯ2を海水に吸収させ、処理後のガスを大気中に放出するものである。上記排気ガスと海水との接触により、下記（ａ）から（ｄ）に示すような反応が生じると考えられている。
（ａ）ＳＯ2＋Ｈ2Ｏ→ＨＳＯ3 -＋Ｈ+
（ｂ）ＨＳＯ3 -＋１／２Ｏ2→＋ＳＯ4 2-＋Ｈ+
（ｃ）ＣＯ2＋Ｈ2Ｏ→ＨＣＯ3 -＋Ｈ+
（ｄ）ＨＣＯ3 -→ＣＯ3 2-＋Ｈ+ The case where the exhaust gas generated by burning fossil fuel is subjected to seawater desulfurization will be described. The exhaust gas generated by burning fossil fuel contains sulfur in the form of SO 2 or the like. The exhaust gas desulfurization apparatus makes exhaust gas and seawater come into gas-liquid contact, absorbs SO 2 in the exhaust gas into seawater, and releases the processed gas into the atmosphere. It is considered that the following reactions (a) to (d) occur due to the contact between the exhaust gas and seawater.
(A) SO 2 + H 2 O → HSO 3 − + H +
(B) HSO 3 − + 1 / 2O 2 → + SO 4 2− + H +
(C) CO 2 + H 2 O → HCO 3 − + H +
(D) HCO 3 − → CO 3 2− + H +

上記のように、排気ガスと海水との気液接触により亜硫酸（ＳＯ3）を酸化させて硫酸（ＳＯ4）の形態に変えて安定させるようにしているが、単に排気ガスを海水と気液接触させたのみではＳＯ3を完全には酸化させることができず、よって硫黄吸収海水（排液）には多くのＳＯ3が含まれている。 As described above, sulfur dioxide (SO 3 ) is oxidized by gas-liquid contact between the exhaust gas and seawater to be changed into the form of sulfuric acid (SO 4 ), but the exhaust gas is simply converted into seawater and gas-liquid. Only by contacting, SO 3 cannot be completely oxidized, and therefore sulfur-absorbing seawater (drainage) contains a large amount of SO 3 .

このため、上記排液に新たな海水を混合してｐＨを高めた混合液を生成し、この混合液にエアレーション（曝気）を行うことによってＳＯ3の酸化を促進させ、化学的酸素要求量（ＣＯＤ）を所定値以下に低減すると共に溶存酸素（ＤＯ）を所定値以上に高めることが行われている。 For this reason, fresh seawater is mixed with the effluent to produce a liquid mixture having an increased pH, and the aeration (aeration) is performed on the liquid mixture to promote the oxidation of SO 3 , and the chemical oxygen demand ( COD) is reduced below a predetermined value, and dissolved oxygen (DO) is increased above a predetermined value.

上記したような海水脱硫は操業方法が簡単であるため実用性に優れており、上記海水脱硫について技術開示した先行技術情報には、例えば特許文献１、２等がある。   Seawater desulfurization as described above is excellent in practicality because of its simple operation method, and examples of prior art information technically disclosed regarding the seawater desulfurization include Patent Documents 1 and 2, for example.

特開２００６−５５７７９号公報JP 2006-55779 A 特開平０９−１７３７６９号公報JP 09-173769 A

従来の硫黄を含有する排液を処理するための曝気槽では、小径の空気吹出口から空気を噴出させて微細気泡を形成することによって混合液との接触面積を増大させ、これによってＳＯ3の酸化を促進させると共に、ＣＯＤ及びＤＯが要求値になるようにしている。 In a conventional aeration tank for treating a waste liquid containing sulfur, air is ejected from a small-diameter air outlet to form fine bubbles, thereby increasing the contact area with the liquid mixture, thereby increasing the SO 3 concentration. While promoting oxidation, COD and DO are set to the required values.

しかし近年、国によってはＣＯＤが今までの国内基準に対して１桁低いオーダーの要求値を設定している場合があり、又、ＤＯについても厳しい要求値が設定される場合がある。これに対し、前記したような微細気泡を混合液と接触させるようにした曝気槽では、特に曝気開始直後においてＳＯ3の酸化が進まないという問題があると共に、全体的なＳＯ3の酸化促進効果が低いという問題があり、よってＣＯＤ及びＤＯの厳しい要求値に対してクリアすることが困難であるという問題を有していた。 However, in recent years, depending on the country, COD may have set a required value that is an order of magnitude lower than the domestic standard so far, and there may be a strict required value for DO. On the other hand, in the aeration tank in which the fine bubbles as described above are brought into contact with the mixed solution, there is a problem that the oxidation of SO 3 does not proceed particularly immediately after the start of aeration, and the overall SO 3 oxidation promotion effect. Therefore, it is difficult to meet the strict requirements of COD and DO.

本発明は、上記従来の問題点に鑑みてなしたもので、簡略な装置構成にて硫黄を含有する排液のＳＯ3の酸化を促進させ、ＣＯＤを所定値以下に低減すると共にＤＯを所定値以上に高めることができるようにした海水脱硫装置を提供することを目的とする。 The present invention has been made in view of the above-described conventional problems, and promotes the oxidation of SO 3 in waste liquid containing sulfur with a simple apparatus configuration, reduces COD to a predetermined value or less, and sets DO to a predetermined value. It aims at providing the seawater desulfurization apparatus which enabled it to raise more than a value.

本発明は、硫黄を含有する排液に海水を混合してｐＨを５．７〜６．５に調整した混合液を生成する混合槽と、該混合槽の混合液を導入し底部に備えた空気管の複数の吹出口から空気を噴出して曝気を行う曝気槽とを有する海水による脱硫装置であって、前記空気管に備える空気吹出口の口径を２ミリメートル以上としたことを特徴とする海水脱硫装置、に係るものである。   The present invention is provided with a mixing tank for producing a mixed liquid in which seawater is mixed with waste liquid containing sulfur to adjust the pH to 5.7 to 6.5, and the mixed liquid in the mixing tank is introduced at the bottom. A desulfurization apparatus using seawater having an aeration tank for performing aeration by ejecting air from a plurality of outlets of an air pipe, wherein the diameter of the air outlet provided in the air pipe is 2 mm or more This relates to a seawater desulfurization apparatus.

上記海水脱硫装置において、前記空気吹出口の口径が３〜５ミリメートルであることは好ましい。   In the seawater desulfurization apparatus, the air outlet preferably has a diameter of 3 to 5 millimeters.

上記海水脱硫装置において、前記排液が、排気ガスと海水等を気液接触して排気ガス中に含まれる硫黄を吸収除去した吸収塔からの硫黄吸収海水であることは好ましい。   In the seawater desulfurization apparatus, it is preferable that the waste liquid is sulfur-absorbing seawater from an absorption tower obtained by gas-liquid contact between exhaust gas and seawater to absorb and remove sulfur contained in the exhaust gas.

本発明によれば、曝気槽に設置される空気管に備えられる空気吹出口の口径を２ミリメートル以上としたので、空気吹出口から吹き出された空気の気泡が曝気槽の混合液内を上昇する上昇力によって混合液が効果的に攪拌され、これによって、曝気開始直後でも硫黄の酸化が促進されると共に、ＣＯＤ及びＤＯの厳しい要求値が達成できるようになるという優れた効果を奏し得る。   According to the present invention, since the diameter of the air outlet provided in the air pipe installed in the aeration tank is 2 mm or more, the air bubbles blown out from the air outlet rise in the mixed liquid in the aeration tank. The mixed solution is effectively agitated by the ascending force, whereby the oxidation of sulfur is promoted even immediately after the start of aeration, and an excellent effect that strict requirements of COD and DO can be achieved can be achieved.

本発明を実施する形態の一例としての海水脱硫装置の概略を示す全体側面図である。It is a whole side view showing the outline of the seawater desulfurization device as an example of the embodiment which carries out the present invention. 図１の廃液処理装置の平面図である。It is a top view of the waste liquid processing apparatus of FIG. 図２の側面図である。FIG. 3 is a side view of FIG. 2. 図３のＩＶ−ＩＶ矢視図である。It is the IV-IV arrow line view of FIG. 空気管の断面図である。It is sectional drawing of an air pipe. 混合液のｐＨと曝気槽でのＳＯ3の酸化速度との関係を調査した試験結果を示すグラフである。The relationship between the oxidation rate of SO 3 in pH and aeration tank of the mixture is a graph showing the test results of the investigation. 空気管の空気吹出口の口径とＳＯ3の酸化速度との関係を調査した試験結果を示すグラフである。Is a graph showing the test results of investigating the relationship between the oxidation rate of the aperture and SO 3 in the air outlet of the air pipe.

以下、本発明の実施の形態を添付図面を参照して説明する。   Embodiments of the present invention will be described below with reference to the accompanying drawings.

図１〜図５は本発明を実施する形態の一例を示すもので、図１は海水脱硫装置の概略を示す全体側面図であり、図１中１は吸収塔である。吸収塔１は、火力発電設備等からの硫黄を含む排気ガス２を下部のガス入口３から導入して海水との気液接触により硫黄を吸収除去し、清浄になった出口ガス４を上部のガス出口５から排出するようになっており、更に、海水６を受け入れて貯留する海水ピット７の海水６を、海水ポンプ８により前記吸収塔１に設けたスプレーノズル９に供給して吸収塔１内に噴射することにより前記排気ガス２と気液接触させて排気ガス２の脱硫を行うようになっている。   1 to 5 show an example of an embodiment for carrying out the present invention. FIG. 1 is an overall side view showing an outline of a seawater desulfurization apparatus, and 1 in FIG. 1 is an absorption tower. The absorption tower 1 introduces an exhaust gas 2 containing sulfur from a thermal power generation facility or the like through a lower gas inlet 3 and absorbs and removes sulfur by gas-liquid contact with seawater. Further, the seawater 6 in the seawater pit 7 that receives and stores the seawater 6 is supplied to the spray nozzle 9 provided in the absorption tower 1 by the seawater pump 8 to absorb the seawater 6. The exhaust gas 2 is brought into gas-liquid contact with the exhaust gas 2 to be desulfurized.

前記吸収塔１で排気ガス２の脱硫を行った硫黄を含む排液１０は、図１〜図３に示す廃液処理装置１１に導いて排液処理を行うようになっている。前記海水ピット７は、図示しない火力発電所等の主機コンデンサからの海水（凝縮海水）又は海洋からの海水６を前端（図２、図３では左端）の海水取入口１２から取り入れるようになっている。海水ピット７は後方（右側）へ向かって平面左右幅（図２では上下）が末広がり状に拡大された形状を有しておりその後端部底面には堰１３が設けられている。そして、海水ピット７の海水６は堰１３を乗り越えて後方へ流出するようになっている。ここで、海水ピット７の深さは例えば２．３メートルであり、堰１３の高さは例えば０．９メートルとなっている。前記海水ピット７の側部には張出部１４が連通して形成されており、この張出部１４に前記海水ポンプ８が設置されている。   The waste liquid 10 containing sulfur obtained by desulfurizing the exhaust gas 2 in the absorption tower 1 is guided to the waste liquid treatment apparatus 11 shown in FIGS. The seawater pit 7 takes in seawater (condensed seawater) from a main condenser such as a thermal power plant (not shown) or seawater 6 from the sea from a seawater intake 12 at the front end (left end in FIGS. 2 and 3). Yes. The seawater pit 7 has a shape in which the horizontal width in the plane (upper and lower in FIG. 2) is widened toward the rear (right side), and a weir 13 is provided on the bottom surface of the rear end. And the seawater 6 of the seawater pit 7 flows over the weir 13 and flows backward. Here, the depth of the seawater pit 7 is, for example, 2.3 meters, and the height of the weir 13 is, for example, 0.9 meters. An overhanging portion 14 is formed in communication with the side of the seawater pit 7, and the seawater pump 8 is installed in the overhanging portion 14.

前記海水ピット７の後部には、海水ピット７と同じ深さを有し、且つ後方（右側）へ向かって平面左右幅が末広がり状に拡大された混合槽１５が設けてあり、該混合槽１５の底部には、前記吸収塔１の排液１０を導く排液供給管１６が混合槽１５の左右幅方向に延設して設けてあり、該排液供給管１６の長手方向には所要の間隔を有して流出口１７が形成されて前記排液１０が流出するようになっている。排液供給管１６は直径が例えば１８００ミリメートルであり、流出口１７の口径は例えば３５０〜３７０ミリメートルとなっている。   At the rear of the seawater pit 7, a mixing tank 15 having the same depth as that of the seawater pit 7 and having a laterally wide width toward the rear (right side) is provided so as to widen toward the rear. A drainage supply pipe 16 that guides the drainage liquid 10 of the absorption tower 1 extends in the left-right width direction of the mixing tank 15, and the drainage supply pipe 16 has a required length in the longitudinal direction. An outlet 17 is formed with an interval so that the drainage 10 flows out. The drainage supply pipe 16 has a diameter of, for example, 1800 millimeters, and the diameter of the outlet 17 is, for example, 350 to 370 millimeters.

更に、前記混合槽１５の後部には、図２〜図４に示すように、前記海水ピット７及び混合槽１５と同等の深さを有する曝気槽１８が形成されており、曝気槽１８の底部には、左右幅方向に延びた例えば２００Ａの空気管１９が前後方向に所要の間隔で多数配設されている。そして、前記空気管１９はコンプレッサ等の加圧空気供給装置２０に接続されている。２１は曝気槽１８の後部底面に備えた堰であり、この堰２１の高さは例えば１．５メートルとなっている。   Further, as shown in FIGS. 2 to 4, an aeration tank 18 having a depth equivalent to the seawater pit 7 and the mixing tank 15 is formed at the rear of the mixing tank 15, and the bottom of the aeration tank 18 is formed. For example, a large number of air tubes 19 of 200A, for example, extending in the left-right width direction are arranged at a required interval in the front-back direction. The air pipe 19 is connected to a pressurized air supply device 20 such as a compressor. Reference numeral 21 denotes a weir provided on the bottom of the rear portion of the aeration tank 18, and the height of the weir 21 is, for example, 1.5 meters.

前記空気管１９には、図５に示すように、空気管１９の中心を通る鉛直線に対して前後６０゜の位置に、口径が２ミリメートル以上（例えば３〜５ミリメートル）の空気吹出口２２が、空気管１９の長手方向に例えば９０ミリメートルの間隔で形成されている。   As shown in FIG. 5, the air pipe 19 has an air outlet 22 having a diameter of 2 millimeters or more (for example, 3 to 5 millimeters) at a position of 60 ° front and rear with respect to a vertical line passing through the center of the air pipe 19. Are formed at intervals of, for example, 90 millimeters in the longitudinal direction of the air pipe 19.

前記曝気槽１８は、前後長さが例えば２４メートル、左右幅が例えば２０メートルとなっている。前記曝気槽１８の後部には処理後の海水を排水する排出口２３が設けられており、更に、排出口２３の上流位置には新鮮な海水６'を供給して混合するための海水供給管２４が設けられている。尚、図２、図３における２５は混合槽１５で排液１０と海水６が混合されて曝気槽１８に導かれる混合液であり、２６は前記混合液２５のｐＨを検出するｐＨ計であり、２７は海水取入口１２に設けて海水６の取入を調節するための海水取入ゲートである。   The aeration tank 18 has a longitudinal length of, for example, 24 meters and a lateral width of, for example, 20 meters. A discharge port 23 for draining the processed seawater is provided at the rear of the aeration tank 18, and a seawater supply pipe for supplying fresh seawater 6 ′ to the upstream position of the discharge port 23 for mixing. 24 is provided. 2 and 3, reference numeral 25 denotes a mixed liquid in which the waste liquid 10 and seawater 6 are mixed in the mixing tank 15 and led to the aeration tank 18, and 26 is a pH meter for detecting the pH of the mixed liquid 25. , 27 is a seawater intake gate provided at the seawater intake 12 for adjusting the intake of the seawater 6.

次に、上記図示例の作動を説明する。   Next, the operation of the illustrated example will be described.

図１に示す吸収塔１の下部のガス入口３には火力発電設備等からの硫黄を含んだ排気ガス２が供給される一方、前記海水ピット７の海水６が海水ポンプ８によりスプレーノズル９に供給されて噴射することにより、吸収塔１内で排気ガス２と海水６の気液接触が行われて排気ガス２の硫黄が海水に吸収除去される。   An exhaust gas 2 containing sulfur from a thermal power generation facility or the like is supplied to a gas inlet 3 at the lower part of the absorption tower 1 shown in FIG. 1, while seawater 6 in the seawater pit 7 is fed to a spray nozzle 9 by a seawater pump 8. By being supplied and injected, the gas-liquid contact between the exhaust gas 2 and the seawater 6 is performed in the absorption tower 1, and the sulfur in the exhaust gas 2 is absorbed and removed by the seawater.

吸収塔１内で硫黄を吸収した排液１０は、図２、図３に示すように排液供給管１６により混合槽１５に導かれて流出口１７から混合槽１５内に噴出し、海水ピット７から供給される海水６と混合されることにより混合液２５となる。この時、混合液２５のｐＨを検出するｐＨ計２６の検出ｐＨが５．７〜６．５になるように、前記排液供給管１６から供給される排液１０に対して海水ピット７に取り込む海水６の取り込み量を海水取入ゲート２７により調節する。   As shown in FIGS. 2 and 3, the drainage liquid 10 that has absorbed sulfur in the absorption tower 1 is guided to the mixing tank 15 through the drainage supply pipe 16, and is ejected from the outlet 17 into the mixing tank 15. 7 is mixed with seawater 6 supplied from 7. At this time, the pH meter 26 for detecting the pH of the mixed solution 25 is fed to the seawater pit 7 with respect to the drainage 10 supplied from the drainage supply pipe 16 so that the detected pH is 5.7 to 6.5. The amount of the seawater 6 to be taken in is adjusted by the seawater intake gate 27.

前記したように吸収塔１において排気ガス２と海水６とが気液接触する際にはＨ+が発生し、これが海水に溶け込むために排液のｐＨは下がることになる。操業条件等にもよるが、多量の硫黄とＣＯ2分を吸収して生じる排液のｐＨは３程度になっている。 As described above, when the exhaust gas 2 and the seawater 6 come into gas-liquid contact in the absorption tower 1, H + is generated, and this dissolves in the seawater. Although it depends on the operating conditions, the pH of the effluent generated by absorbing a large amount of sulfur and CO 2 is about 3.

このため、混合槽１５において混合液２５のｐＨが例えば５．７〜６．５になるように調整して曝気槽１８に導き、曝気槽１８の底部に設けた空気管１９の空気吹出口２２からコンプレッサ等の加圧空気供給装置２０により供給される空気を噴出させることにより曝気を行う。このとき、加圧空気供給装置２０から供給する空気は、混合液２５の水頭圧に打ち勝って空気を噴出できる圧力に調整されている。   For this reason, it adjusts so that pH of the liquid mixture 25 may be set to 5.7-6.5 in the mixing tank 15, for example, it guides to the aeration tank 18, and the air blower outlet 22 of the air pipe 19 provided in the bottom part of the aeration tank 18 Aeration is performed by ejecting air supplied from a pressurized air supply device 20 such as a compressor. At this time, the air supplied from the pressurized air supply device 20 is adjusted to a pressure capable of overcoming the head pressure of the mixed liquid 25 and ejecting the air.

ここで、本発明者らは、曝気槽１８に導く混合液２５のｐＨと曝気槽１８でのＳＯ3の酸化速度との関係を、ＳＯ3濃度が１０ｍｇ／ｌの混合液２５を用いて調査する試験を実施し、その結果を図６に示した。 Here, the present inventors investigated the relationship between the pH of the liquid mixture 25 guided to the aeration tank 18 and the oxidation rate of SO 3 in the aeration tank 18 using the liquid mixture 25 having an SO 3 concentration of 10 mg / l. The test was conducted and the results are shown in FIG.

図６に示すように、ＳＯ3の酸化速度係数（Ｋ）はｐＨが６前後の５．７〜６．５において最も高い値を示した。 As shown in FIG. 6, the oxidation rate coefficient (K) of SO 3 showed the highest value at 5.7 to 6.5 where the pH was around 6.

従って、曝気槽１８に導く混合液２５のｐＨが５．７〜６．５になるように、混合槽１５において排液１０と海水６の混合割合を調節すると、曝気槽１８におけるＳＯ3の酸化は効果的に促進されることが判明した。ここで、通常の海水６のｐＨは８前後であるため、混合槽１５においてこの海水６と排液１０を混合してｐＨを調整する際には大量の海水６が必要であることから、海水６の混合量を少なく押えるために混合液２５のｐＨは５．８前後に設定することが好ましい。 Therefore, when the mixing ratio of the drainage liquid 10 and the seawater 6 is adjusted in the mixing tank 15 so that the pH of the mixed liquid 25 guided to the aeration tank 18 is 5.7 to 6.5, the oxidation of SO 3 in the aeration tank 18 is performed. Was found to be effectively promoted. Here, since the pH of the normal seawater 6 is around 8, a large amount of seawater 6 is necessary when adjusting the pH by mixing the seawater 6 and the drainage 10 in the mixing tank 15. In order to keep the mixing amount of 6 small, the pH of the liquid mixture 25 is preferably set to around 5.8.

又、本発明者らは、曝気槽１８に設けられる空気管１９の空気吹出口２２の口径とＳＯ3の酸化速度との関係を調査する試験を実施し、その結果を図７に示した。図７に示すように、ＳＯ3の酸化速度係数（Ｋ）は空気吹出口２２の口径が小さいと低い値を示し、口径が大きくなると高い値を示しており、特に口径が２ミリメートル或いは３ミリメートルにおいて略ピーク値を示し、その後は口径が大きくなっても酸化速度係数（Ｋ）は殆ど上昇しないことが判明した。 In addition, the inventors conducted a test to investigate the relationship between the diameter of the air outlet 22 of the air pipe 19 provided in the aeration tank 18 and the oxidation rate of SO 3 , and the result is shown in FIG. As shown in FIG. 7, the oxidation rate coefficient (K) of SO 3 shows a low value when the diameter of the air outlet 22 is small, and shows a high value when the diameter is large, especially the diameter is 2 millimeters or 3 millimeters. It was found that the oxidation rate coefficient (K) hardly increased even when the aperture was increased.

従って、曝気槽１８に備える空気管１９の空気吹出口２２の口径を２ミリメートル以上に設定すると、曝気槽１８におけるＳＯ3の酸化は効果的に促進されることが判明した。ここで、空気吹出口２２の口径を大きくすると、混合液２５の水頭圧に打ち勝って空気を噴出させるための空気圧が増加しコンプレッサ等の加圧空気供給装置２０が大型化することから空気吹出口２２の口径は小さい方が好ましく、よって、空気吹出口２２の口径は３ミリメートル前後に設定することが好ましい。 Therefore, it has been found that when the diameter of the air outlet 22 of the air pipe 19 provided in the aeration tank 18 is set to 2 mm or more, the oxidation of SO 3 in the aeration tank 18 is effectively promoted. Here, if the diameter of the air outlet 22 is increased, the air pressure for overcoming the water head pressure of the liquid mixture 25 and ejecting air increases, and the pressurized air supply device 20 such as a compressor becomes larger. The diameter of 22 is preferably smaller, and therefore the diameter of the air outlet 22 is preferably set to around 3 millimeters.

又、前記したように空気吹出口２２の口径を３ミリメートルに設定した時の空気吹出口２２から吹き出される空気によって混合液２５中に形成される気泡口径について調査したところ、平均径が約７ミリメートルの気泡が発生していることが判明した。従って、このように７ミリメートル前後の気泡が混合液２５内を上昇することによる上昇力によって混合液２５が効果的に攪拌されることによりＳＯ3の酸化が効果的に促進されたものと考えられる。 In addition, as described above, the bubble diameter formed in the mixed liquid 25 by the air blown out from the air outlet 22 when the diameter of the air outlet 22 is set to 3 millimeters was investigated. It was found that millimeter bubbles were generated. Therefore, it is considered that the oxidation of SO 3 was effectively promoted by the effective stirring of the mixed solution 25 by the ascending force caused by the bubbles of about 7 millimeters rising in the mixed solution 25. .

このように、曝気槽１８でＳＯ3の酸化が促進された処理後の海水は、ＣＯＤが０．５ｍｇ／ｌ以下、ＤＯが５ｍｇ／ｌとなっており、よってＣＯＤ及びＤＯの厳しい要求値に対して十分に対応することができる。 In this way, the seawater after the treatment in which the oxidation of SO 3 is promoted in the aeration tank 18 has a COD of 0.5 mg / l or less and a DO of 5 mg / l. It is possible to respond sufficiently.

又、処理後の海水はそのまま排出口２３から海洋に排出するようにしてもよいが、図２、図３に示すように海水供給管２４からの新鮮な海水６'を混合してｐＨ等の調整を行った後に排出するようにしてもよい。   The seawater after the treatment may be discharged directly from the discharge port 23 to the ocean. However, as shown in FIGS. 2 and 3, fresh seawater 6 ′ from the seawater supply pipe 24 is mixed to adjust the pH and the like. You may make it discharge | emit after adjusting.

なお、本発明は上記形態のみに限定されるものではなく、本発明の要旨を逸脱しない範囲内において種々変更を加え得ることは勿論である。   In addition, this invention is not limited only to the said form, Of course, a various change can be added in the range which does not deviate from the summary of this invention.

１ 吸収塔
２ 排気ガス
６ 海水
１０ 排液
１５ 混合槽
１８ 曝気槽
１９ 空気管
２２ 空気吹出口
２５ 混合液 DESCRIPTION OF SYMBOLS 1 Absorption tower 2 Exhaust gas 6 Seawater 10 Drainage 15 Mixing tank 18 Aeration tank 19 Air pipe 22 Air outlet 25 Mixed liquid

Claims (3)

硫黄を含有する排液に海水を混合してｐＨを５．７〜６．５に調整した混合液を生成する混合槽と、該混合槽の混合液を導入し底部に備えた空気管の複数の吹出口から空気を噴出して曝気を行う曝気槽とを有する海水による脱硫装置であって、前記空気管に備える空気吹出口の口径を２ミリメートル以上としたことを特徴とする海水脱硫装置。   A mixing tank for producing a mixed liquid in which seawater is mixed with sulfur-containing wastewater to adjust the pH to 5.7 to 6.5, and a plurality of air pipes provided at the bottom by introducing the mixed liquid in the mixing tank A seawater desulfurization apparatus having an aeration tank for performing aeration by ejecting air from the air outlet, wherein the air outlet provided in the air pipe has a diameter of 2 mm or more. 前記空気吹出口の口径は３〜５ミリメートルである請求項１に記載の海水脱硫装置。   The seawater desulfurization apparatus according to claim 1, wherein the diameter of the air outlet is 3 to 5 mm. 前記排液は、排気ガスと海水等を気液接触して排気ガス中に含まれる硫黄を吸収除去した吸収塔からの硫黄吸収海水である請求項１又は２に記載の海水脱硫装置。   The seawater desulfurization apparatus according to claim 1 or 2, wherein the waste liquid is sulfur-absorbing seawater from an absorption tower in which exhaust gas and seawater are brought into gas-liquid contact to absorb and remove sulfur contained in the exhaust gas.
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